Mother Liquor Research Articles

Conversion of Harmful Fly Ash Residue to Zeolites: Innovative Processes Focusing on Maximum Activation, Extraction, and Utilization of Aluminosilicate.

Reuse of the solid residue from coal fly ash alumina extraction (FAAE) by acid leaching is problematic. Conversion of this solid residue into aluminum-rich zeolite (13X) and silicon-rich zeolite (ZSM-5) was investigated in this research. The FAAE residue was activated by alkali roasting with Na2CO3 powder (110% mass fraction) at 890 °C for 60 min. Silicon and aluminum were mainly present as two mineral phases, Na2SiO3 and NaAlSiO4, respectively, in the product obtained after roasting. The roasted product was dissolved in water (liquid/solid ratio of 2) after 20 min at 100 °C. The water-leaching liquor was investigated for total conversion to aluminosilicate zeolites without external aluminum or silicon addition. Hydrothermal synthesis of aluminum-rich zeolite 13X was successful after fine tuning of the conditions, although the filtrate had an unusually high SiO2/Al2O3 molar ratio. Production of 13X consumed a large amount of aluminum, which increased the Si/Al ratio to a level suitable for synthesis of ZSM-5. The synthesis of ZSM-5 from the mother liquor of 13X was proved feasible. The FAAE residue was transformed into high-value zeolite products by nearly 100%. Additionally, the tail liquid of this process, mainly containing Na2CO3, was completely recycled. This process could be used to realize high-efficiency and high-value utilization of similar aluminosilicate solid wastes.

Ammoniacal nitrogen removal and reuse: Process engineering design and technoeconomics of zeolite N synthesis

This investigation of Zeolite N synthesis addressed process flow design and manufacturing economics. Zeolite N is important as it has high selectivity and capacity for ammonium ions which means it has applications in wastewater treatment or nutrient management. The aim was to accelerate zeolite N use by developing an optimal economic model for zeolite N synthesis. Three process designs for 30 tonnes per day zeolite N production were evaluated; (1) No recycling of mother liquor or wash water; (2) recycling of mother liquor; (3) recycling of mother liquor and wash water. Recycling strategies reduced demand for KOH & KCl by 58% and 83%, respectively. Water consumption was lowest for the mother liquor/wash water recycling plant (c.f. 185 m3 per batch compared to 290 m3 per batch for base case). Similarly, wastewater generation was least when using the mother liquor/wash water recycling approach. Capital expenditure was similar for the three processes (A$14,190,750 to A$15,504,000). However, operational expenditure was considerably less when recycling mother liquor and wash water. The highest net present value (NPV) for zeolite N synthesis resulted from internal recycling of mother liquor and first stage wash water (A$85,813,532) resulting in a payback period of 2.44 years. Notably the assumed zeolite N selling price of A$2000 per tonne was less than the literature value of A$3067 per tonne which was suggested to be economically attractive. Sensitivity analysis indicated a break-even point of A$1300 per tonne of zeolite N and that zeolite price was the major factor controlling project viability.

Separation and extraction of niobium from H2SO4 solution containing titanium and iron impurities

A fluoride-free solvent extraction method for niobium separation in leached sulfuric mother liquor of ilmenorutile was proposed in this paper. The extraction system comprising trioctyl tertiary amine (N235) and 4-methyl-2-pentanone (MIBK) demonstrated good extraction efficiency and selectivity of niobium over titanium and iron impurities in sulfuric acid–oxalate solutions. Details of extraction, scrubbing, and stripping processes were investigated herein, and its practical effectiveness in both batch and multi-stage simulated counter-current modes was verified. Over 73.8% niobium was extracted under optimum conditions, and only 2.8% titanium and 1.7% iron were co-extracted. The recovery of niobium reached 99.1% in the four-stage simulated counter-current extraction tests. In the three-stage simulated counter-current stripping tests, the stripping efficiency of niobium reached 99.7% with 2.0 mol/L HNO3. Qualified niobium oxide products were prepared. The enthalpy change, entropy change, and the standard Gibbs free energy change (ΔHo, ΔSo, and ΔGo, respectively) corroborated the exothermicity, orderliness, and spontaneity of the reaction. The possible composition of the extraction complex was [NbO(C2O4)2(H2O)2]−, as supported by a Fourier transform infrared spectroscopy and ultraviolet–visible spectrophotometry. The extraction mechanism was inferred to be the outer-sphere complexation through physical binding which was the association of R3NH+ in N235 with the [NbO(C2O4)2(H2O)2]−. A preliminary mass balance indicated that 203.92 g Nb2O5 was generated from 1000 g raw material ilmenorutile.

Conversion from α-spodumene to intermediate product Li2SiO3 by hydrothermal alkaline treatment in the lithium extraction process

The key to the lithium extraction from α-spodumene is destroying the crystal structure. The conventional commercial process requires high-temperature calcination to transform α-spodumene into β-spodumene. This study aimed at finding an alternative treatment for destroying the structure of α-spodumene and extracting the lithium. The results indicated that α-spodumene could be directly decomposed by NaOH solution and the Li element in α-spodumene was converted into intermediate product Li2SiO3 in the form of solid phase under certain conditions. According to the experiments, the possible reactions during the hydrothermal alkaline treatment were predicted, which were thermodynamically possible by the calculation of Gibbs free energy using HSC Chemistry 10. The total extraction efficiency of Li2O was 87.3%, including the extraction efficiency of Li2O leached into liquid phase, 7.6%, and converted into Li2SiO3, 79.7%, obtained under optimal conditions: stirring speed of 500 rpm, leaching temperature of 250 °C, mass ratio of NaOH/ore of 1.5, initial NaOH concentration of 25 wt%, and leaching time of 24 h. Then the Li element in the Li2SiO3 could be extracted by acid leaching and precipitated using Na2CO3. The mother liquor obtained after hydrothermal alkaline treatment was reused for the subsequent hydrothermal alkaline cyclic leaching under the above conditions. During three cycles of alkaline treatment, the α-spodumene decomposition was stable, and the total Li2O extraction efficiency was around 86% (∼84% was converted into Li2SiO3). This process avoids high-temperature calcination and concentrated acid roasting, where the acid leaching process is carried out at room temperature.

Synthesis of Magnesium Hydroxide Using Post‐Reaction Filtrate as Ammonia Carrier and Morphology Analysis

AbstractThis study proposes an advanced technology using post‐reaction filtrate as an ammonia carrier to synthesize magnesium hydroxide (MH) with small particles, which can benefit subsequent hydrothermal modification. In this work, the limitation of ammonia gas and ammonia water methods is avoided. The impact of operating parameters including MgCl2 concentration, temperature, ammonia‐to‐magnesium molar ratio, feed rate, volume of ammonia mother liquor and aging time on the magnesium yield, particle size, and morphology of MH is studied. The temperature and ammonia‐to‐magnesium molar ratio are identified as key factors affecting magnesium yield. MH with a half‐content diameter of 1.70 µm and a morphology resembling small irregular flakes is successfully synthesized at a magnesium yield of 90.06%. The predictions of idea crystal habits are also performed using Morphology and CASTEP modules with Materials Studio Software. The (0 0 1) face can be preserved with the largest facet area because of the slowest crystal growth rate and the smallest attachment energy, which exhibits that MH crystals tend to be flakes.

Processing of Metallic Bismuth and Production of Bismuth Compounds

This paper demonstrates the efficiency of dissolving metallic bismuth in 7 mol/L nitric acid in the presence of 325–558 g/L ammonium nitrate to produce nitric acid solutions. Thus, solutions with 415–450 g/L bismuth can be obtained while the transition of nitrogen oxides in the gas phase can be decreased from 66 to 0.01 % and more. The obtained solutions were treated by bismuth precipitation in the first stage. Thus, the solutions with the following composition: [Bi6O4(OH)4](NO3)6·H2O – were 10 times diluted with water at the temperature of 60±3 oC, then they were rinsed with water resulting in the following compound: [Bi6O5(OH)3](NO3)5·3H2O. The product was then dried at 100 oC and baked at 630±30 oC into high-purity oxides. Bismuth was precipitated from the mother and wash liquors by adding a 2.5 mol/L ammonium carbonate solution at 55 oC until рН = 1 was reached. The precipitate was rinsed with water, dried and baked resulting in the production of chemically pure bismuth oxides. It is shown that the following oxohydroxo nitrates: [Bi6O4(OH)4](NO3)6·H2O and [Bi6O5(OH)3](NO3)5·3H2O – produced as a result of metallic bismuth processing can be used as precursors of high-purity bismuth compounds when interacting with acidic or alkaline solutions. Based on the results of the conducted study, an eco-friendly process was developed for Ви1 grade metallic bismuth containing at least 98% of bismuth. The process involves dissolving bismuth in nitric acid in the presence of ammonium nitrate, processing of bismuth-containing solution by water-alkali hydrolysis. At the water hydrolysis stage, 81.8 % of bismuth is recovered as high-purity bismuth oxides. At the same time, 15.1 % of bismuth is recovered as chemically pure bismuth oxides when hydrolysis is conducted with an ammonium carbonate solution at рН = 1. Due to final precipitation of bismuth from the solution at рН = 3 in the form of oxohydroxo nitrate and that of lead, silver and copper at рН = 8 while sending bismuth oxohydroxo nitrate and the ammonium nitrate solution to the metallic bismuth dissolution stage, a minimum 99.9 % of bismuth, as well as the ammonium nitrate solution, can be utilized at the metallic bismuth processing stage. The transition of nitrogen oxides in the gas phase during metallic bismuth dissolution does not exceed 0.01 %.

A Nrf-2 Stimulatory Hydroxylated Cannabidiol Derivative from Hemp (Cannabis sativa).

A phytochemical analysis of mother liquors obtained from crystallization of CBD from hemp (Cannabis sativa), guided by LC-MS/MS and molecular networking profiling and completed by isolation and NMR-based characterization of constituents, resulted in the identification of 13 phytocannabinoids. Among them, anhydrocannabimovone (5), isolated for the first time as a natural product, and three new hydroxylated CBD analogues (1,2-dihydroxycannabidiol, 6, 3,4-dehydro-1,2-dihydroxycannabidiol, 7, and hexocannabitriol, 8) were obtained. Hexocannabitriol (8) potently modulated, in a ROS-independent way, the Nrf2 pathway, outperforming all other cannabinoids obtained in this study and qualifying as a potential new chemopreventive chemotype against cancer and other degenerative diseases.

Removing trace chromium from high concentration vanadium solution by photoreduction deposition with Ti–Zr solid solution

The preparation of ultrahigh-purity vanadium (>99.99 wt%) requires the removal of trace amounts of chromium, but economical vanadium purification is difficult to achieve using crude vanadium mother liquors (>98 wt%) because of the similar properties of V(V) and Cr(IV) ions. In this study, a Ti–Zr solid solution was used for the deep purification of high-concentration ammonium polyvanadate by removing trace chromium using photocatalytic reduction process. The results show that V(V) and Cr(VI) are competitively adsorbed and photoreduced, but V(V) adsorption is preferred and occurs more rapidly than that of Cr(VI). However, after the photoreduction product of V(V), V(IV) is desorbed, whereas after that of Cr(VI), Cr(III) is deposited on the photocatalyst, achieving the separation of vanadium and chromium. The 2 h removal efficiency of chromium exceeds 80%, and the chromium content in the obtained vanadium is less than 0.04 wt%. After precipitation, the chromium content in the obtained ammonium metavanadate is less than 0.001 wt%, and the purity of the final V2O5 product exceeds 99.99%, which meets the requirement for ultrahigh-purity vanadium products. The used photocatalyst can be regenerated and reused with stable performance. This work provides a reference method for ultrahigh-purity vanadium production and an example of the industrial application of the photoreduction process.

Features of the crystallization of AlCl3·6H2O in the system AlCl3 – MeClx – HCl – H2O

A laboratory setup has been developed to study the regularities of crystallization of aluminium chloride hexahydrate from hydrochloric acid solutions. The influence of the AlCl3 content in the initial solution, the consumption of gaseous HCl, and the behavior of impurities on the crystallization of AlCl3·6H2O from aluminium chloride solutions of leaching cinder obtained as a result of chlorinating ash burning from thermal power plants in Kazakhstan have been studied. The behavior of impurity metals in the process of crystallization of aluminium chloride solution has been studied, and their distribution between the products of the crystallization process has been established. It is shown that aluminium chloride content in the solution decreases with an increase in the consumption of hydrochloric acid. It was found that under the conditions of crystallization of AlCl3·6H2O, all impurities, except for barium, pass by 98% into the mother liquor. To reduce barium and other impurities in the obtained crystals of AlCl3·6H2O, it is proposed to carry out multiple washing of the crystals with hydrochloric acid (32% HCl). It has been shown that a decrease in the acidity of the washing solution from pH = 10 to pH = 5.5 ensures the isolation of ACH crystals with a minimum content of impurity metals, ppm: 3-5 Ca; 3-6 Fe; 1-3 Mg; 0.1-0.5 Ti; 1-3 Na; 20-30 P2O5. The moisture content of the obtained crystals is 4-5%; the particle size is 400-900 microns. As a result of mathematical processing, regression equations were constructed that adequately predict aluminium chloride content in the solution and its extraction into crystalline hydrate, depending on the consumption of hydrochloric acid. The optimal parameters of the crystallization process have been established: Т = 60 ºС, HCl concentration in the solution - 26-30%, HCl gas consumption = 0.5 l/min, duration 1 hour.

Laboratory suspension freeze concentration (Lab SFC) followed by a simple centrifugal procedure for separation

Suspension freeze concentration (SFC) is a low temperature technology which has a promising prospect in food and bioproducts industry. In SFC, the dispersed ice crystals are made in aqueous fluid and become bigger in sizes after ripening, are then separated from the mother liquor to achieve ice removal. A laboratory device of 2 L capacity integrating ice nucleation and ripening in one pot has been investigated in this study. Centrifugation is then applied to the whole slurry (in contrast to a tightly packed ice phase in previous studies) to separate the liquid out, which simplifies greatly the SFC process. This procedure was successfully used to concentrate sucrose solution from 10oBrix (wt%) to 17.6oBrix (wt%). For the first time, Scanning Electron Microscopy (SEM) was used to look at the microscopic distribution of sucrose attached and partly included in the ice particles. The solute loss (sucrose inclusion in the ice phase) was further reduced to only 0.6oBrix (wt%) by partially melting the particle phase. The yield of solute reached to about 97% in one go of about 2 hours. Agitation, partial ice melting, etc., were also examined in the current work. Similarly, the solid contents of orange juice, skim milk and the red wine can be concentrated to similar levels in runs of about 1.5 hours. This work has shown that this laboratory scale device is nice and simple for concentrating small amounts of practical aqueous liquids. The centrifuge as it is adopted here is also simple to operate and the whole procedure shows great promise for practical applications.

Isolation, synthesis, identification of new process-related impurities in evocalcet

Evocalcet is a calcimimetic for the treatment of secondary hyperparathyroidism. In the preparation of evocalcet, eleven process-related impurities were detected in the reaction solution of the last step at levels of 0.05%− 2.50% by a new HPLC method. Ten impurities were separated from the enriched mother liquor and synthesized directly. These impurities were characterized and identified by HRMS and NMR spectra and then coinjected with commercial products to confirm their retention times in HPLC. The possible formation pathways and synthetic methods of ten process-related impurities ware discussed in detail.

Mathematical Model of Mother Liquor Deposition in Industrial Sugar

Mathematical Model of Mother Liquor Deposition in Industrial Sugar

Ultra-permeable high-selective SAPO-34 membranes for efficient CO2 capture

Ultra-permeable SAPO-34 membranes with membrane thickness of 0.8–1.2 μm were reproducibly fabricated using diluted mother liquids with H2O/Al2O3 ratios of 300 and 450. The orientation and thickness of the membranes were greatly affected by mother liquid dilution. Thickness-even SAPO-34 membranes were reproducibly prepared in a large synthesis time window, indicating that membrane synthesis had good robustness and it is suitable to the scale-up fabrication. The membranes prepared at H2O/Al2O3 ratio of 450 displayed ultrahigh CO2 permeances of (1.0–1.3) × 10−5 mol (m2 s Pa)−1 (∼30000–37000 GPU) and CO2/CH4 selectivities of (56–126) at 298 K and 0.2 MPa pressure drop. The typical membrane also displayed CO2 permeance of 7.6 × 10−6 mol (m2 s Pa)−1 (∼23000 GPU) and CO2/N2 selectivity of 35 for an equimolar CO2/N2 mixture. The separation performance of these thin SAPO-34 membranes was far beyond that of most reported membranes. Such CO2 permeances of the membranes are 200–350 times higher than that of commercial polyimide membranes. The membranes shows great potentials for CO2 capture from natural and flue gases.

Sustainable research methodology for potassium nitrate recovery from seawater

Since centuries, seawater has been a natural resource to recover NaCl, KNO3, KCl and other salts along with many other resources. The present study reports KNO3 recovery from seawater bittern by averting kainite, KMg(SO4)Cl·3H2O, schoenite, K2Mg(SO4)2·6H2O and carnallite, KCl·MgCl2·6H2O mixed complex salts formation by adding NaNO3. Reported KCl recovery via hazardous thermal decomposition of these salts has been modified to recover KNO3 instead of KCl using green routes. The NaNO3 widened salt solubilities have facilitated a faster evaporation with better crystal nucleation sequentially, giving end liquor for continued recovery as per solubility. Continued evaporation of hydrated ionic seawater bittern has recovered 96.26% KNO3, 97.19% NaCl, and 98.93% MgCl2.6H2O by disrupting hydration spheres. Solvay Process Effluent (SPE) CaCl2 has desulfated the SO42− ions from respective mother liquor and NaNO3 by reengineering the resultant ionic hydration spheres which had fastened evaporation. Desulfation separated CaSO4.2H2O leaving filtrate as mother liquor having KNO3, NaCl and MgCl2.6H2O. NaNO3 addition to this mother liquor has catalyzed KNO3 nucleation by engineering cohesive forces of Na+-Cl− and NO3−-K+ hydration spheres on a sustained evaporation in evaporation compartment. Industrial sustainability of NaNO3 route has been the recovery of CaSO4.2H2O, NaCl, MgCl2.6H2O, MgO, HCl and precipitated SiO2, a safer alternative of hazardous thermal decomposition.

Tungsten extraction from scheelite hydrochloric acid decomposition residue by hydrogen peroxide

• W was leached from crude tungstic acid or residue by an efficient and clean method. • H 2 O 2 dissolved W from crude tungstic acid or residue selectively. • The W leaching ratio exceeded 96% for crude tungstic acid and 99% for the residue. • Pure tungstic acid was obtained from peroxotungstic acid solution. • More than 99.6% of W was precipitated from peroxotungstic acid solution. To reduce the amount of ammonia wastewater produced during traditional tungsten metallurgy, a novel method has been developed. Hydrogen peroxide was first used to selectively dissolve tungsten from crude tungstic acid and scheelite hydrochloric acid decomposition residue. Then, the peroxotungstic acid solution obtained was heated to prepare pure tungstic acid through thermal decomposition . The results showed that when the temperature was 40–45 °C, the molar ratio of hydrogen peroxide to tungstic acid was 2:1, and the reaction time was 60 min, more than 96 % of the crude tungstic acid was dissolved. Tungsten was easily leached from the hydrochloric acid decomposition residue under the conditions of a hydrogen peroxide concentration of 1.95 mol/L, 60 min, and 30 °C. The tungsten leaching ratio was 99.4 %. Using a decomposition temperature higher than 95 °C, seed addition amount more than 2.5 g/L, an acid concentration of 1 mol/L, and a reaction time of 120 min, the final W concentration in the mother liquor was 0.5 g/L and the decomposition ratio of peroxotungstic acid was more than 99.6 % with the product being WO 3 ·H 2 O. This research showed that hydrogen peroxide could dissolve tungstic acid and scheelite hydrochloric acid decomposition residue, and that the peroxotungstic acid obtained was readily decomposed into tungstic acid, which made it possible to leach scheelite cleanly and efficiently.

A green approach to improve the yield of SAPO-34 crystal as well as its methanol-to-olefin performance

Nowadays, large amounts of aluminosilicophosphate SAPO-34 zeolite are produced in industrials annually. Here, a green strategy is developed to increase SAPO-34 crystal's yield and its catalytic performance in methanol-to-olefin (MTO) reaction. Tuning the pH value of mother liquor from alkaline to acid by rationally decreasing the environmentally unfriendly organic amine to only 57%, surprisingly the yield of SAPO-34 zeolite increases from 31% to 78%; the weak acid environment at the initial stage generates more AlPO4 precursors, which then are converted into the zeolite framework. For the first time, we found that the yield and crystallinity of the SAPO-34 crystal are positively correlated with the pH difference between gels before and after crystallization. Furthermore, the sample with the largest pH difference of about 2, showing hierarchical pore structure and mild acidity, presents excellent MTO performance: a longer lifetime of 381 ​min and a higher selectivity for ethylene plus propylene of 84.91%, compared to the conventional microporous sample of 131 ​min and 78.89%. This green approach uses less environmentally detrimental amine but enhances the yield of zeolite, in favor of the completion of the world's carbon neutrality.

Global reprogramming of xylose metabolism in Saccharomyces cerevisiae efficiently produces ethanol from lignocellulose hydrolysates

The biggest challenge of utilizing lignocellulosic feedstocks for efficient ethanol fermentation is to improve strains and processes capable of mixed sugar fermentation in the presence of released inhibitors. A previously reported Saccharomyces cerevisiae strain WXY70 was further engineered to overexpress up to eight xylose metabolic genes or a transcription factor SPT2, and their efficacy in fermentation was evaluated in a simulated corn hydrolysate, resulting in two favored strains 8G-3 and SPT2OE. SPT2OE produced 0.503 and 0.508 g ethanol/g total sugars in ball milling-based and corn hydrolysates, respectively, within 24 h. Moreover, SPT2OE produced about 40 g/L ethanol from 120 g/L xylose mother liquid solution. Overall, the fermentation performance of SPT2 overexpression was superior to recently reported SFA1 overexpression and achieved promising results of ethanol yield and titer in different hydrolysates.

A Simple Population Balance Model for Crystallization of L-Lactide in a Mixture of n-Hexane and Tetrahydrofuran

In this contribution, crystallization was performed to assess the kinetics of nucleation and crystal growth of L-lactide. In most common solvents, this compound shows very high solubility even at low temperatures, which could be challenging for crystallization process design. In the first part of this paper, the anti-solvent effects of n-hexane on solutions of L-lactide in tetrahydrofuran (THF) were investigated through studying the influence of solvent compositions on the solubility. Thanks to these effects, the solubility of the interested compound can be adjusted to desired degrees of supersaturation by adding suitable amounts of the anti-solvent. In the second part, a solvent composition at a mass ratio of 45/55 (n-hexane/THF) was chosen, and an isothermal seeded crystallization process was implemented. The evolution of the particle sizes and changes in the solute concentration profile of this process were monitored. Based on the obtained data, a widely used model, i.e., the population balance equation (PBE), was then utilized to model the crystal size distribution (CSD). Reasonable assumptions were made to reduce the mathematical complexity of the PBE. In the simplified model, only crystal growth and secondary nucleation were considered for model formulation, with assumptions of the size-independent growth rate and negligible size of nuclei. The kinetic parameters were estimated by using the seed and final-time crystal density functions in combination with variations in the concentration of the mother liquor. Indeed, the numerical solution for the one-dimensional problem of the L-lactide crystallization based on the estimated parameters gained a relatively good agreement with the determined CSD. Furthermore, the obtained model also correlated well with the variations in the solute concentration of the mother liquor. In short, this simple approach can be used for predicting the productivity and CSD of the L-lactide crystallization.

K-4 Impact on Dehydration Process of Red Mud Settling

The article represents the results of a study on the red mud dehydration process (thickening, filtration, filtration washing) obtained in the alumina production during the processing of the low-silica bauxites. The synthetic flocculant K-4 has been used in order to intensify the red mud dehydration process. The main washing periods have been studied in the process of the filtration washing analysis. The expendable module impact on the effectiveness of aluminate solution cleaning (mother liquor) obtained from the mud settling has been represented. The settling washing, treated by the flocculant, has been established to allow increasing the quantity of the specific effective moisture at the cost of the mutual volume of the standing pores and the grow of free moisture volume.

A novel and sustainable technique to precipitate vanadium from vanadium-rich solutions via efficient ultrasound irradiation

During the traditional acidic ammonium salt precipitation process of vanadium, a large amount of ammonium salt is commonly consumed, hence high-concentration ammonia nitrogen wastewater is inevitably produced, which poses a great threat to the environment. In this investigation, a novel and environmentally friendly technique adopting ultrasound to strengthen the ammonium salt precipitation process of vanadium is firstly put forward and investigated. Under the optimal conditions, the precipitation percentage of vanadium and V2O5 purity of the ultrasound precipitation (UP) products can reach 99.67% and 99.50%, respectively, which is similar to the results of the regular precipitation (RP) process. However, the most obvious advantages of the former are that the reaction time can be dramatically shorten from 25 min to 5 min and the amount of ammonium salt consumption can be decreased by as much as 87.5% with the intensification of ultrasound. Both UP and RP methods are capable of preparing pure (NH4)2V6O10, but the UP products exhibit more uniform size distribution and smaller mean particle diameter (9.88 μm vs 46.2 μm) compared to the RP products. The microstructure analysis demonstrates that the UP products have more regular crystal shape, where the fine flake crystals intercalate with each other in comparison to the latter. The precipitation kinetics analysis demonstrates that the intensification of ultrasound mainly embodies in the increase of the collision frequency of NH4+ and vanadium, which further accelerates the nucleation and growth rate of the precipitated crystals. Particularly, the residual NH4+ concentration in the precipitated mother liquor can be observably reduced from 24449 mg/L to 1083 mg/L using the UP method. In short, the proposed technique can definitely promote the green and sustainable development of vanadium extraction industry.